CN101712661A - Method for producing epoxy chloropropane - Google Patents
Method for producing epoxy chloropropane Download PDFInfo
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- CN101712661A CN101712661A CN200910250001A CN200910250001A CN101712661A CN 101712661 A CN101712661 A CN 101712661A CN 200910250001 A CN200910250001 A CN 200910250001A CN 200910250001 A CN200910250001 A CN 200910250001A CN 101712661 A CN101712661 A CN 101712661A
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Abstract
The invention relates to a method for producing epoxy chloropropane. The method comprises the steps of mixing of dichloropropanol isomer mixed solution and Ca(OH)2 emulsion, dehydrochlorination, saponification and cyclization reaction, product separation and purification, wastewater treatment of reaction distillation column bottom fraction process, and the like. The method of the invention has the advantages of simple and convenient process flow, easy operation and cost, low equipment investment and obvious economic benefit. The yield of the epoxy chloropropane in the method can reach over 95 percent, and meanwhile the content of COD in the process wastewater produced by the dehydrochlorination, saponification and cyclization reaction is lower compared with the prior art; therefore, the method of the invention is a method with high epoxy chloropropane yield and byproduct environmental protection, and has quite appreciable application prospect.
Description
[technical field]
The invention belongs to the chemical products technical field.More specifically, the present invention relates to a kind of production method of epoxy chloropropane.
[background technology]
Epoxy chloropropane has another name called Epicholorohydrin, is important Organic Chemicals, is mainly used in to produce Resins, epoxy, glass reinforced plastic, electrically insulating material, tensio-active agent, medicine, agricultural chemicals, coating, ion exchange resin, softening agent, chlorohydrin rubber.
At present, epoxy chloropropane traditional industry production method has propylene high-temperature chlorination process and allyl acetate method, and the former throughput is 95% of global overall throughput, and the allyl acetate method only is 3%.Along with the rise of biofuel, be that the raw material production epoxy chloropropane has entered the industrial technology field at present as the third method with its by-product glycerin.The end reaction of these three kinds of methods all is to be raw material with the dichlorohydrine that obtains, and carries out the reaction of dehydrochlorination and saponification cyclization under alkaline environment, generates epoxy chloropropane.
According to traditional be in the dichlorohydrine production method of raw material with propylene and chlorine, the dichloropropanol isomer that is obtained by the propenyl chloride hypochlorination mainly is 2.3-two trimethylewne chlorohydrin 3-s.
Allyl acetate clear according to Japan and the exploitation of electrician company is in the dichlorohydrine production method of raw material, and the dichlorohydrine that is obtained by vinylcarbinol and chlorine addition all is 2.3-two trimethylewne chlorohydrin 3-isomer basically.
Solvay ﹠ Cie (Societe Anonyme) discloses a kind of method of producing dichlorohydrine by glycerine in Chinese patent application CN 200480034393.2, wherein spell out this method has height to 1.3-two chloro-2-propyl alcohol selectivity.
Have now and studies show that the 1.3-two chloro-2-propyl alcohol of generation are the 95-98% of dichlorohydrine total amount when producing dichlorohydrine by glycerine, 2.3-two trimethylewne chlorohydrin 3-s are 2-5% of dichlorohydrine total amount.
Chinese patent application CN 200480034393.2 has described in the process of producing Epicholorohydrin, preferably uses NaOH, Ca (OH)
2Strong solution etc. at least a alkali; And described and to have reclaimed enrichment salt by evaporation or reverse osmosis.Enrichment salt gold-plating branch can reclaim, and randomly is used for for example producing the electrolyzer of chlorine after suitable purification step.
Jiangsu Polytechnic University has described in CN 200810020885.6 and has used 10% to 40%NaOH solution to carry out the saponification cyclization reaction, and the epoxy chloropropane yield can reach 81-83%.
DOW Chemical fine chemistry (Shanghai) Co., Ltd. plans to build 120,000 tons of/year glycerine method epoxy chloropropane projects, in " publicity is estimated in the project environment influence ", mention: under the effect at catalyzer, glycerine and HCl carry out chlorination reaction, generate dichlorohydrine, dichlorohydrine again with the sodium hydroxide solution reaction that is hydrolyzed, generate epoxy chloropropane.
Clear and the electrician JP 1988017874A of Japan, reviving into DE 4229355A1 etc., all to relate to propylene and chlorine be raw material production dichlorohydrine (being mainly 2.3-two trimethylewne chlorohydrin 3-s), and then the method for epoxy chloropropane is produced in cyclization, wherein mention " using calcium hydroxide that the dichlorohydrine cyclization is epoxy chloropropane; stripping under the steam ", not mentioned calcium hydroxide surface property.
At present, on the one hand, existing documents and materials and patent application open be raw material production dichlorohydrine (being mainly 1.3-two chloro-2-propyl alcohol) with glycerine and hydrogenchloride, again and then cyclization when producing epoxy chloropropane, all do not mention cyclizing agent NaOH, Ca (OH)
2Alkali lye is to the influence of cyclization side reaction and method productive rate.
On the other hand, in epoxy chloropropane was produced, dehydrochlorination and saponification cyclization reaction can produce a large amount of waste water, and contain high density NaCl or CaCl
2Deng organism such as inorganics and glycerine, adopt present normally used biochemical method to handle these waste water and be difficult to reach the relevant waste water standard of country; The moisture gold-plating branch that adopts reverse osmosis to reclaim the enrichment salt, the especially NaCl that obtain will be paid very high production cost, have not yet to see industrialized report.
Encircling all ages in the Guangzhou, Environmental Projects Inc., the big chemical industrial company in east, Shandong, the living building materials of Shandong Zibo treasured company limited etc. all adopt the waste water that will contain calcium chloride and a small amount of glycerine to concentrate through multiple-effect evaporation earlier, after calcium chloride concentration reaches 65-68%, reclaim Calcium dichloride dihydrate through flaker crystallization and fluidised bed drying again.Because glycerine boiling point height after organism such as the glycerine in the waste water are brought the Calcium dichloride dihydrate product into, makes the CODcr content in the product reach 1.65%.Such Calcium dichloride dihydrate can cause the pollution to environment when using as Snow Agent.
Therefore, also be starved of a kind of epoxy chloropropane productive rate height of development at present, the environment amenable method of by product.
[summary of the invention]
[technical problem that will solve]
The production method that the purpose of this invention is to provide a kind of epoxy chloropropane is comprising the treatment step of processing wastewater that this method produces.
[technical scheme]
The present invention is achieved through the following technical solutions.
The present invention relates to a kind of production method of epoxy chloropropane.This method steps is as follows:
With the dichloropropanol isomer mixed solution of 900-1000 weight part, the water of 950-1050 weight part, the HCl of 70-100 weight part and the Ca (OH) of 2600-2800 weight part
2Content is that the lime slurry of 12-18 weight % mixes, and is added to reactive distillation column top behind the mixing; Described Ca (OH)
2The particulate specific surface area is 200-2100m
2/ kg, median size 1.8-20.0 μ m;
The water vapor that feeds the 1100-1300 weight part at the bottom of described reactive distillation column carries out the reaction of dehydrochlorination saponification cyclization, simultaneously described reaction distillation capital temperature is controlled at 86-90 ℃;
Then, collect described reaction distillation column top fractions, and in condenser, carry out condensation, obtain phlegma; Cut is a processing wastewater at the bottom of the described reactive distillation column, handles;
Described phlegma is separated, and obtains containing the organic phase and the water of epoxy chloropropane, and described water turns back in the described reactive distillation column;
Then, described organic phase sent among the knockout tower I under absolute pressure 0.12-0.14MPa condition, separate, isolate light by-product and be rich in epichlorohydrin product; Described light by-product is discharged from knockout tower I cat head, discharges at the bottom of this tower as tower bottom distillate and be rich in epichlorohydrin product, and described tower bottom distillate is again by being pumped into knockout tower II;
Described tower bottom distillate separates under absolute pressure 36-40KPa condition in described knockout tower II, isolates residual light by-product, pure epoxy chloropropane product and heavy byproduct; Described residual light by-product is discharged from knockout tower II cat head, and described pure epoxy chloropropane is discharged from knockout tower II tower side, is target product of the present invention, and described heavy byproduct waste liquid is discharged at the bottom of the knockout tower II tower and handled.
According to a preferred embodiment of the present invention, described dichloropropanol isomer mixed solution is the product that the glycerine method is produced dichlorohydrine, this mixture contains in 1 of its mixture total weight amount 95-98 weight %, the 2.3-two trimethylewne chlorohydrin 3-isomer of 3-two chloro-2-propyl alcohol isomer and 2-5 weight %.
In the present invention, described Ca (OH)
2The particulate specific surface area is 726-765m preferably
2/ kg.
Described Ca (OH)
2The median size of particulate is 5.3-4.6 μ m preferably.
The invention still further relates to described processing wastewater treatment process, this method steps is as follows:
Described processing wastewater carries out evaporation concentration by quintuple effect evaporator earlier, is concentrated into calcium chloride content and reaches in concentrating spent liquor gross weight 50 weight %CaCl
2
The concentrating spent liquor that obtains carries out crystallisation by cooling, separates out the calcium chloride hexahydrate crystal, carries out filtering separation then;
Separate the calcium chloride hexahydrate crystal that obtains and heat, obtain calcium chloride water, carry out spraying drying again, obtain Calcium Chloride Powder Anhydrous;
Simultaneously, separate the crystalline mother solution that contains glycerine and organic chloride that obtains and carry out burning disposal.
According to a preferred embodiment of the present invention, it is 0.7-0.9MPa that described quintuple effect evaporator uses the absolute pressure of heating steam, the secondary steam absolute pressure 0.018-0.022MPa of quintuple effect evaporator, the total temperature difference of described quintuple effect evaporator is 108-109 ℃, 52.5-53.5 ℃ of total temperature difference loss, effective temperature difference 54.5-56.5 ℃.
According to another preferred embodiment of the present invention, described concentrating spent liquor carries out crystallisation by cooling under temperature 15-21 ℃.
According to another preferred embodiment of the present invention, described calcium chloride hexahydrate crystal heated 20-30 minute under temperature 30-35 ℃, obtained calcium chloride water.
According to another preferred embodiment of the present invention, described calcium chloride solution carries out spraying drying in 350 ℃ of temperature and pressure 50-200pa direct draught.
The present invention will be described in detail belows.
The present invention relates to a kind of production method of epoxy chloropropane.
The step division of this method is as follows:
One, dichloropropanol isomer mixed solution and Ca (OH)
2Emulsion is mixed
The present invention allows the mixed solution of 1.3-two chloro-2-propyl alcohol and a small amount of 2.3-two trimethylewne chlorohydrin 3-s and alkali lye carry out the reaction of dehydrochlorination saponification cyclization in a kind of reactive distillation column (described reaction combines with sepn process), produce epoxy chloropropane, used here alkali lye is Ca (OH)
2Emulsion, the process of producing can produce and contain higher concentration CaCl
2With contain gold-plating branch at the bottom of the organic towers such as glycerine.
The present invention is with Ca (OH)
2Emulsion is as dehydrochlorination saponification alkali lye, with NaOH solution as dehydrochlorination saponification caustic liquid phase ratio, have higher yield.
Following reaction takes place in dichlorohydrine under the alkali lye environment:
(1) dichlorohydrine generates epoxy chloropropane under alkaline environment, and its reaction is as follows:
(2) epoxy chloropropane of Sheng Chenging and water react, and generate glycerine monochloro alcohol, and its reaction is as follows:
(3) the glycerine monochloro alcohol that is generated is easy to be hydrolyzed into Racemic glycidol and glycerine under alkaline environment, its reaction is as follows:
Above-mentioned these reactions are carried out in a reactive distillation column, are the technological processs that chemical reaction and sepn process are carried out simultaneously.Above-mentioned (1) group reaction resultant is the purpose product, and (2) group reaction is and the placed in-line side reaction of (1) group reaction that (3) group reaction is (2) group reaction by product hydrolysis reaction.The present invention utilizes the centrifugation of reaction distillation, and purpose product epoxy chloropropane is come out from alkaline liquid phase environment stripping as soon as possible, reduces follow-up side reaction.The present invention relates to the relation between chemical kinetics and the diffusion control is optimized.Those skilled in the art know that described stripping process is a heat and mass diffusion process, and it determines with transmission impellent, flow pattern and melange effect, the influence of entrainment state transitivity.Therefore, require the speed of reaction of A+B → C and the heat and mass speed of process to be complementary, speed of reaction is too fast, will cause the purpose product to rest on for a long time in the process system, and the side reaction of C → D will be inevitable.
Existing studies show that used glycerine, when hydrogenchloride prepares dichlorohydrine, and by weight, 1.3-two chloro-2-propyl alcohol isomer are 95-98% of dichlorohydrine ultimate production, and 2.3-two trimethylewne chlorohydrin 3-s are 2-5% of dichlorohydrine ultimate production.
What is more important, in alkaline environment, 1.3-the reactivity ratio 2.3-two trimethylewne chlorohydrin 3-isomer of the dehydrochlorination saponification cyclization of two chloro-2-propyl alcohol isomer reaction are stronger, have speed of reaction faster, that is to say, 1.3-two chloro-2-propyl alcohol are that the conversion zone length of saponification reaction distillation tower of raw material is shorter, and the reaction product epoxy chloropropane gathers at conversion zone, concentration is higher, to enter put forward the gold-plating section after, epoxy chloropropane concentration slowly reduces.The residence time of product epoxy chloropropane in tower is longer, therefore helps the epoxy chloropropane hydrolysis reaction.
The present invention is intended to reduce the chemical reaction rate impellent according to the requirement of diffusion control process, specifically, is intended to be reduced in the OH in the reaction system of the present invention
-Concentration.The saponification reagent that is prepared epoxy chloropropane by dichlorohydrine can be selected NaOH, Ca (OH)
2Or other alkali.The inventor is with the Ca (OH) of document record
2Dissolubility data in water is listed in the table below in 1:
Table 1
| Temperature (℃) | Solubleness (gram Ca (OH) 2/ 100 gram H 2O) |
| ??40??60??80??100 | ??0.141??0.116??0.094??0.077 |
As shown in Table 1, Ca (OH)
2Solubleness in water is very little.But people know that NaOH is ionization fully in the aqueous solution, therefore, under same strength of solution, the OH of NaOH
-Concentration ratio Ca (OH)
2Much higher.
So the present invention selects to use Ca (OH)
2As saponification reagent, its limited lysate in water can make it keep suitable almost lasting supplies OH
-Ability.
Ca (OH)
2Emulsion need be with active OH when participating in the reaction of dehydrochlorination saponification cyclization
-Be controlled in the suitable scope.The inventor studies show that, under reaction conditions of the present invention, and active OH
-Rate of release just with emulsion in Ca (OH)
2The particulate specific surface area is relevant.The Ca of the embodiment of the invention 3 (OH)
2The particulate specific surface area is too small, active OH
-Release rate too slow, and the 2.3-two trimethylewne chlorohydrin 3-activity that are dichlorohydrine total amount 5% are relatively poor, cause 2.3-two trimethylewne chlorohydrin 3-s residence time in liquid phase to prolong like this, 2.3-two trimethylewne chlorohydrin 3-s and epoxy chloropropane generate chlorine ether, form more organic chloride by product.In addition, in the reaction distillation process, 2.3-two trimethylewne chlorohydrin 3-s are stripped in the thick epoxy chloropropane product with reaction product, thereby reduce product yield.
Determine through a large amount of tests, in the present invention with the dichloropropanol isomer mixed solution of 900-1000 weight part, the water of 950-1050 weight part, the HCl of 70-100 weight part and the Ca (OH) of 2600-2800 weight part
2Content is that the lime slurry of 12-18 weight % mixes, and adds in the reactive distillation column behind the mixing.
In the present invention, dichloropropanol isomer mixed solution should be appreciated that it is the dichloropropanol isomer mixed solution of using glycerine in the prior art, obtaining when hydrogenchloride prepares dichlorohydrine, promptly by the mixture of forming in dichloropropanol isomer mixed solution gross weight 95-98 weight %1.3-two chloro-2-propyl alcohol isomer and 2-5 weight %2.3-two trimethylewne chlorohydrin 3-s.
In the present invention, Ca (OH)
2Emulsion is the powdery Ca (OH) that sells with in the market
2Preparation.Described Ca (OH)
2The particulate specific surface area is 200-2100m
2/ kg.For the present invention, described Ca (OH)
2The particulate specific surface area can be greater than or less than above-mentioned Ca (OH)
2Particulate specific surface area scope is because use these Ca (OH)
2Particulate be can implement of the present invention, but can influence the productive rate of described epoxy chloropropane product.
Preferably, described Ca (OH)
2The particulate specific surface area is 500-2000m
2/ kg.
More preferably, described Ca (OH)
2The particulate specific surface area is 700-1500m
2/ kg.
Most preferably, described Ca (OH)
2The particulate specific surface area is 726-765m
2/ kg.
In the present invention, described Ca (OH)
2The particulate median size is 1.8-20.0 μ m.For the present invention, described Ca (OH)
2The particulate median size can be greater than or less than above-mentioned Ca (OH)
2The particulate average particle size range is because use these Ca (OH)
2Particulate be can implement of the present invention, but can influence the productive rate of described epoxy chloropropane product significantly.
Preferably, described Ca (OH)
2The particulate median size is 1.8-15.0 μ m.
More preferably, described Ca (OH)
2The particulate median size is 3.9-7.7 μ m.
Most preferably, described Ca (OH)
2The particulate median size is 4.6-5.3 μ m.
In the present invention, described Ca (OH)
2The maximum particle diameter of particulate is 30-100 μ m.For the present invention, described Ca (OH)
2The particulate median size can be greater than or less than above-mentioned Ca (OH)
2The maximum particle diameter scope of particulate is because use these Ca (OH)
2Particulate be can implement of the present invention, but the Ca of maximum particle diameter (OH)
2Particulate is at whole C a (OH)
2Ratio in the particulate should be very little, along with Ca (OH)
2Diameter of particle is big more, and described ratio should be more little.If the excessive productive rate that will inevitably influence described epoxy chloropropane product of this ratio.
In the present invention, described Ca (OH)
2Particulate specific surface area, median size and maximum particle diameter are to use laser particle size distribution instrument and analogous instrument thereof to measure, for example the BT-9300H type laser particle size distribution instrument of selling as Dandong Baite Science and Technology Co., Ltd..
Two, carry out the reaction of dehydrochlorination saponification cyclization
Described in front dichloropropanol isomer mixed solution and Ca (OH)
2Emulsion mixes the back and adds described reactive distillation column top, and the water vapor that feeds the 1100-1300 weight part simultaneously at the bottom of the described reactive distillation column carries out the reaction of dehydrochlorination saponification cyclization, and described reaction distillation capital temperature is controlled at 86-90 ℃;
In the present invention, described reactive distillation column is the equipment that those skilled in the art know, and these equipment for example adopt mode that present people know that the temperature and the mass flow of reactive distillation column are controlled in the claimed range of the present invention.
Then, collect described reaction distillation column top fractions, this cut contains and is about 96% thick epoxy chlorine chlorine alkane, and cut is a processing wastewater at the bottom of the described reactive distillation column, mainly contains in processing wastewater gross weight 10-12 weight %CaCl
2, 0.5-0.8 weight %CaCO
3And Ca (OH)
2, 0.3-0.8 weight % glycerine and organic chloride, surplus is a water, therefore, can deliver to subsequent processing steps to this waste water and handle.
The cut of discharging from described reactive distillation column top carries out condensation condenser, obtain phlegma.In the present invention, described condensation should be appreciated that it is to allow water coolant or other heat-eliminating medium and described cut carry out heat exchange and condensation that described cut is reached, realizes that the employed equipment of this condensation is condenser.It also is operable adopting other any type of cooling to make described cut condenser condensing.
Then, described phlegma need be separated.In the present invention, described being separated should be appreciated that it is the process that organic phase phase state mixed with water is separated into two single phase states, and for example centrifugal, clarification is separated etc.The described equipment that uses that is separated for example is whizzer, mixer-settlers etc.Described being separated obtains organic phase and water, through gas chromatographic analysis, described organic phase contains a large amount of epoxy chloropropane and a spot of other heavy byproduct, for example propylene dichloride, trichloropropane and other organochlorine, water contains other organochlorine of a large amount of water and a small amount of epoxy chloropropane, dichlorohydrine and less amount, and described water turns back in the described reactive distillation column.
In the present invention, described gas chromatographic analysis is to use An Jielun 6890N gas chromatograph, and the mode that adopts those skilled in the art to know under 220 ℃ of vaporizers, 120 ℃ of column temperatures, 220 ℃ of conditions of detector is analyzed.
Three, product isolation and purification
Above-mentioned organic phase also needs to separate, and removes other light by-product.
In the present invention, described organic phase is separated two sections separation of employing, promptly uses knockout tower I and knockout tower II.
These two knockout towers adopt the rectifying mode to separate, be atmospheric distillation and the negative pressure rectifying separation tower that those skilled in the art know, for example as Wuxi Taihu Petrochemical Equipment Plant and Shandong dragon Xinghua construction machinery Group Co.,Ltd with trade(brand)name rectifying tower product sold.Certainly, organic phase of the present invention is separated and also can be adopted any other separating device to separate, for example as the extracting and separating tower.
In the present invention, knockout tower I be under condition of normal pressure, carry out isolating.
Knockout tower II be under condition of negative pressure, carry out isolating.Described negative pressure should be appreciated that it is absolute pressure 36-40KPa.
The above-mentioned organic phase that obtains of being separated delivered among the knockout tower I separate, be separated into light by-product and be rich in epichlorohydrin product.
Described light by-product is discharged from knockout tower I cat head, adopts above-mentioned gas chromatography analysis method to measure, and it mainly contains water, therefore can drain.
The described epichlorohydrin product that is rich in is discharged at the bottom of this tower as tower bottom distillate, adopts above-mentioned gas chromatography analysis method to measure, and it also contains the heavy by product of dichlorohydrine, trichloropropanol and organochlorine, therefore, must with pump it be sent into knockout tower II again.
Described tower bottom distillate is separated into residual light by-product, pure epoxy chloropropane product and contains the heavy byproduct of dichlorohydrine, trichloropropanol and organochlorine in described knockout tower II.
Described residual light by-product is discharged from knockout tower II cat head, adopts above-mentioned gas chromatography analysis method to measure, and it mainly contains water and a small amount of epoxy chloropropane, therefore can drain.
Described pure epoxy chloropropane is discharged from knockout tower II tower side, is target product of the present invention, delivers to epoxy chloropropane product groove, and product is through packing after the assay was approved.
Described heavy byproduct waste liquid carries out burning disposal.
When adopting method of the present invention to produce epoxy chloropropane, calculate the yield that uses dichloropropanol isomer mixed solution production epoxy chloropropane according to following formula:
The epoxy chloropropane (moL) of epoxy chloropropane yield (%)=production/dichloropropanol isomer (moL)
The epoxy chloropropane yield of the inventive method can reach more than 95%, therefore far above the epoxy chloropropane productive rate that reaches usually in the prior art.
Four, the cut processing wastewater is handled at the bottom of the described reactive distillation column
This processing wastewater is because of high saltiness, can't adopt biochemical process to handle, reclaim Calcium dichloride dihydrate through knot sheet crystallization and fluidised bed drying again with known multiple-effect evaporation, the product Calcium dichloride dihydrate contains CODcr and reaches 1.65%, is equivalent to per 100 gram calcium chloride and contains organic pollutant 1.5 grams.When the product Calcium dichloride dihydrate is applied to fields such as Snow Agent, can cause environmental pollution.Therefore, the present invention has developed a kind of new treatment process.
For removing glycerine and the organic chloride in this processing wastewater, the present invention adopts calcium chloride hexahydrate crystallization realization calcium chloride and the separating organic matters method separated out.
Crystallization is the chemical separating operation of classics, and crystallisation process can be isolated high-purity crystal from the considerable solution of foreign matter content.
People know that dense calcium chloride solution can be separated out calcium chloride hexahydrate at low temperatures, and the temperature range that crystallization exists is for being lower than 29.92 ℃.The CaCl of document record
2Solubleness in water is listed in table 2:
Table 2
| Temperature (℃) | Solubleness (gram CaCl 2/ 100 gram H 2O) | Solid-state |
| ??0 | ??59.5 | ??CaCl 2·6H 2O |
| ??10??20??30 | ??65.0??74.5??102 | 102.8 gram CaCl 2/ 100 gram H 2O |
The present invention has carried out in glycerin/water solution CaCl under differing temps
2Solubility test, when glycerol concentration was low, the solubleness of calcium chloride is not significant to be changed.Measurement result is listed in table 3:
Table 3
The process method step of described processing wastewater is as follows:
Described processing wastewater carries out evaporation concentration by quintuple effect evaporator earlier, is concentrated into calcium chloride content and reaches to concentrate waste water gross weight 50 weight %CaCl
2
Described vaporizer is five effect following current tubular evaparators, for example reach mechanical company limited with trade(brand)name " multiple-effect falling film vaporizer " product sold as the high benefit of Wuxi City, Shanghai legendary god of farming machinery company limited with trade(brand)name " five imitate falling-film evaporator " product supplied or Qinhuangdao Xin Yuan water and wastewater industry company limited with trade(brand)name " high-salt wastewater low-temperature multi-effect vaporizer " product supplied.
According to the processing wastewater situation, can select less or more multi-evaporator carry out evaporation concentration, as long as reach to concentrate waste water gross weight 50 weight %CaCl
2
According to a preferred embodiment of the present invention, it is 0.7-0.9MPa that described quintuple effect evaporator uses the absolute pressure of heating steam, the secondary steam absolute pressure 0.018-0.022MPa of quintuple effect evaporator, the total temperature difference of described quintuple effect evaporator is 108-109 ℃, 52.5-53.5 ℃ of total temperature difference loss, effective temperature difference 54.5-56.5 ℃.
Then, described thickened waste is water-cooled to 15-21 ℃, preferably 18-20 ℃, is added to and contains in the calcium chloride hexahydrate crystalline magma, and keep its cooling temperature, most of CaCl
2With CaCl
26H
2The O crystallization is separated out, and separates mother liquor with whizzer, obtains technical pure calcium chloride hexahydrate intermediates, stays in the mother liquor and is removed to be mainly organism that the glycerine form exists.Contain organic mother liquor through calcination processing, remove organism.
Perhaps, contain organic mother liquor and dewater through distillation, steam glycerine then in the distillation tower of a condition of high vacuum degree, the solid abraum salt is removed organism through calcination processing at the bottom of the tower.
Then, calcium chloride hexahydrate heats 20-30 minute calcium chloride down at temperature 30-35 ℃ and can be dissolved in the crystal water of self, obtains calcium chloride water, carries out spraying drying again, obtains Calcium Chloride Powder Anhydrous.
Light by-product is mainly water from knockout tower I cat head, has a small amount of epoxy chloropropane and other low-boiling-point substance, and the process water that can be used as in the production is used.Heavy byproduct is from knockout tower II tower bottom distillate, its amount is about 1 weight % of final product epoxy chloropropane, its composition is epoxy chloropropane, dichlorohydrine, chlorine ether, trichloropropane, treatment process is that the company that is sent to qualification carries out burning disposal, for example Bei Cang environmental protection in Ningbo is given up admittedly and is disposed company limited, Ningbo Dadi Chemical Environmental Conservation Co., Ltd..
[beneficial effect]
Beneficial effect of the present invention: method of the present invention have technical process easy, be easy to operate and control, facility investment is little, economic benefit is obvious; The yield of epoxy chloropropane can reach more than 95%, use sodium hydroxide high more than 6% than prior art as the yield that saponification cyclization reagent can reach, COD content uses sodium hydroxide much lower as the processing wastewater that saponification cyclization reagent place produces than prior art in the processing wastewater that dichlorohydrine dehydrochlorination saponification cyclization reaction simultaneously of the present invention is produced, therefore, method of the present invention is a kind of epoxy chloropropane productive rate height, the environment amenable method of by product.
[description of drawings]
Fig. 1 is the epoxy chloropropane production scheme
The P-1 transferpump, D-1 lime slurry Preparation tank, X-1 mixing tank, T-1 dehydrochlorination saponification cyclization reactive distillation column, C-1 condenser, C-2 phase separator, T-2 knockout tower I, P-2 transferpump, T-3 knockout tower II, D-2 medial launder
[embodiment]
Embodiment 1
Dichlorohydrine mixed solution and milk of lime are mixed in the continuous adding in the back reactive distillation column.The dichlorohydrine mixed solution is the product that the glycerine method is produced dichlorohydrine, it composed as follows: 1.3-two chloro-2-propyl alcohol 950g, 2.3-two trimethylewne chlorohydrin 3-50g, water 1012g, HCl 85g; The milk of lime add-on is content 15 weight %Ca (OH)
2Emulsion 2740g.Described milk of lime is 5.32 μ m by median size, and specific surface area is 726m
2The Ca of/kg (OH)
2Pulvis is formulated.The internal diameter 25mm of the reactive distillation column of built-in 8 * 1.5 Raschig rings, conversion zone stripping section length overall 500mm, smart gold-plating segment length 150mm feeds stripped vapor 1203g at the bottom of the post; Column top temperature is controlled at 88 ℃, capital gold-plating part is carried out condensation in the straight tube condenser under 30 ℃ of water coolings, condensed reaction mixture is separated into two-phase through precipitating, contains the big little water of density organic aqeous and a small amount of epoxy chloropropane of density of epoxy chloropropane.Described water turns back to the smart gold-plating section of this reactive distillation column, and described organic phase is the thick product of epoxy chloropropane, and its analytical results is listed in table 4.
Then, described organic phase sent among the rectifying separation tower I separate, isolate light by-product that is mainly water and the product that is rich in epoxy chloropropane; Described light by-product separates under condition of normal pressure at rectifying separation tower I, discharges from cat head, adopts described gas chromatography analysis method to measure, and it mainly contains water, therefore can drain.
At the bottom of this tower, discharge as tower bottom distillate and be rich in epichlorohydrin product, again by being pumped into knockout tower II;
Described tower bottom distillate separates under the condition of negative pressure of absolute pressure 36-40KPa in rectifying separation tower II, isolates residual light by-product, pure epoxy chloropropane product and contains the heavy byproduct of dichlorohydrine, chlorine ether, trichloropropane and a small amount of epoxy chloropropane.
Described residual light by-product is discharged from knockout tower II cat head, adopts described gas chromatography analysis method to measure, and it mainly contains water and a small amount of epoxy chloropropane, delivers to knockout tower I again and reclaims epoxy chloropropane.Described pure epoxy chloropropane is discharged from knockout tower II tower side, is target product of the present invention, is collected in the product groove; And described heavy byproduct waste liquid is discharged at the bottom of the knockout tower II tower and is handled.
By analysis, this embodiment prepares pure epoxy chloropropane 690 grams.In dichlorohydrine, the yield of epoxy chloropropane is 96.2%.The analytical results of product sees Table 4.
The analytical results of the thick product of table 4 epoxy chloropropane of the present invention
| Density g/cm 3 | ??1.180-1.183 |
| Purity % (wt) | ??99.6 |
| Moisture % (wt) | ??0.02 |
| Colourity/Hazen unit (platinum-cobalt look number) | ??15 |
Wherein:
Density is to adopt the GB/T4472-1984 standard method to measure;
Purity is to adopt the GB/T13097-2007 standard method to measure;
Moisture is to adopt the GB/T6283-1986 standard method to measure;
Chrominance representation platinum-cobalt look number is to adopt the GB/T3143-1982 standard method to measure.
The analytical results of described processing wastewater sees Table 5.
The comparative example 1
Dichlorohydrine mixed solution and white liquor are mixed in the continuous adding in the back reactive distillation column.The dichlorohydrine mixed solution is the product that the glycerine method is produced dichlorohydrine, it composed as follows: 1.3-two chloro-2-propyl alcohol 950g, 2.3-two trimethylewne chlorohydrin 3-50g, water 1012g, HCl 85g; The caustic soda add-on is the solution 1479g of content 30%NaOH.The internal diameter 25mm of the reactive distillation column of built-in 8 * 1.5 the Raschig ring that this comparative example uses, conversion zone stripping section length overall 500mm, smart gold-plating segment length 150mm feeds stripped vapor 1203g at the bottom of the post; Column top temperature is controlled at 88 ℃, and capital gold-plating part is carried out condensation in condenser under 30 ℃ of water coolings, and condensed reaction mixture is a two-phase through centrifugation, contains the big organic phase and the less water of aqueous density of density of epoxy chloropropane.Described water turns back to the smart gold-plating section of this reactive distillation column, and described organic phase is the thick product of epoxy chloropropane, and its analytical results is listed in table 5.
Table 5: the dehydrochlorination saponification cyclization reacts thick product analysis result
| Embodiment 1 | The comparative example 1 | |
| Slightly epoxy chloropropane output (in gram) wherein: dichlorohydrine 1.2.3-trichloropropane and other organochlorine water ring oxygen chloropropane epoxy chloropropane productive rates | ??718.2??2.7??2.7??22.8??690.0??96.2％ | ??665.0??2.5??2.7??21.1??638.7??89.0％ |
| Processing wastewater output (in gram) is wherein: glycerine organochlorine CaCl 2Or NaCl Ca (OH) 2Or NaOH | ??5320.0??22.0??1.1??567.0??30.7 | ??4112.1??74.0??1.3??631.2??10.0 |
Know that by table 5 embodiment 1 compares and can illustrate with comparative example 1, use Ca (OH)
2Effect as saponification cyclization reagent obviously is better than using NaOH as saponification cyclization reagent.
Embodiment 2-5
Carry out according to the same manner, only be to use following milk of lime with embodiment 1:
The milk of lime of embodiment 2 is 20 μ m by median size, and maximum particle diameter is 100 μ m, and specific surface area is 218m
2The Ca of/kg (OH)
2Pulvis is formulated.
The milk of lime of embodiment 3 is 7.7 μ m by median size, maximum particle diameter 40 μ m, and specific surface area is 500m
2The Ca of/kg (OH)
2Pulvis is formulated.
The milk of lime of embodiment 4 is 4.58 μ m by median size, maximum particle diameter 32.4 μ m, and specific surface area is 765m
2The Ca of/kg (OH)
2Pulvis is formulated.
The milk of lime of embodiment 5 is 1.87 μ m by median size, maximum particle diameter 30 μ m, and specific surface area is 2065m
2The Ca of/kg (OH)
2Pulvis is formulated.
The dehydrochlorination saponification cyclization of these embodiment reacts thick product analysis and the results are shown in table 6.
Table 6 dehydrochlorination saponification cyclization of the present invention reacts thick product analysis result
| Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 | |
| ??Ca(OH) 2Pulvis median size μ m Ca (OH) 2Pulvis specific surface area m 2The thick epoxy chloropropane output of/kg (in gram) is wherein: dichlorohydrine chlorine ether 1.2.3-trichloropropane and other organochlorine water ring oxygen chloropropane epoxy chloropropane yields | ??20??218??695.3??3.3??2.5??2.7??21.3??665.5??92.8％ | ??7.7??500??716.4??2.8??0.4??2.7??22.7??687.8??95.9％ | ??4.58??765??718.3??2.7??0.4??2.7??22.7??689.8??96.2％ | ??1.87??2065??718.0??2.7??0.4??2.7??22.8??689.4??96.1％ |
| Waste water output (in gram) is wherein: glycerine dichlorohydrine trichloropropane chlorine ether CaCl 2??Ca(OH) 2 | ??5342.5??39.9??1.8??0.3??1.7??578.2??26.8 | ??5322??22.4??0.3??0.3??0.5??566.8??30.8 | ??5321??20.1??0.4??0.4??0.5??564.6??31.7 | ??5320??21.6??0.4??0.3??0.6??566.7??30.9 |
As can be seen from the above table:
Embodiment 2 shows, uses the excessive Ca (OH) of particle diameter
2During pulvis, the epoxy chloropropane productive rate is low excessively.
Embodiment 1, embodiment 3-4 show, use suitable Ca (OH)
2During the particle diameter of pulvis, the productive rate of epoxy chloropropane is very high, and wherein median size shows best effect when 5.3-4.6 μ m.
Embodiment 5 shows, the Ca (OH) that particle diameter is too small
2Pulvis does not have remarkable influence to the epoxy chloropropane yield.
The comparative example 2
The quintuple effect evaporator that uses the present invention to describe concentrates comparative example 1 processing wastewater that the reaction of dichlorohydrine dehydrochlorination saponification cyclization is produced in reactive distillation column, and what concentrate back waste water consists of 194g CaCl
2/ 100g H
2O and 6g glycerine/100g H
2O.Get this solution 100g, insert in the 150mm pottery ware, be cooled to room temperature, crystallize into Calcium dichloride dihydrate.Separate the back and in ceramic ware, pulverize, place baking oven dry half an hour under 150 ℃ of temperature then, Calcium dichloride dihydrate product 92g, this product color and luster is pale red.Take by weighing Calcium dichloride dihydrate sample 1g, with adopting the HJ/T132-2003 standard behind the distilled water diluting, the potassiumiodide basic potassium permanganate method is measured CODcr, measures to obtain that CODcr content is 2.2% in this Calcium dichloride dihydrate product, amounts to that CODcr content is 2.9% in the Calcium Chloride Powder Anhydrous.
Embodiment 6
The quintuple effect evaporator that uses the present invention to describe, the processing wastewater that the dichlorohydrine dehydrochlorination saponification cyclization reaction that embodiment 1 is obtained is produced concentrates, and concentrates the 100gCaCl that consists of of back waste water
2/ 100g H
2O and 3.1g glycerine/100g H
2O.Get this solution 131.3g, it is divided into two samples, a copy of it is 1/3 amount (sample 1), and another part is 2/3 amount (sample 2), inserts respectively in the beaker of 150ml, then, sample 1 placed at low temperatures, is settled out the calcium chloride hexahydrate crystal.At this moment insert in the water-bath with the beaker that sample 2 is housed separating out calcium chloride hexahydrate crystalline beaker, bath temperature is controlled at 18 ℃, with slow stirring of agitator crystalline solution is arranged, uncrystallized sample 2 solution that have been cooled to 18 ℃ are slowly poured in sample 1 solution, and keeping its solution temperature is 20 ℃, continues 10 minutes, to this solution retrogradation, use vacuumfilter to carry out suction filtration, suction filtration is after 1 hour, with the pure 100g CaCl of 10g
2/ 100g H
2The solution washing filter cake of O.Keep equal 20 ℃ of envrionment temperature when suction filtration and washing.Filter cake and filtrate are weighed respectively, get wet cake 112.3g, filtrate 29g.
Filter cake is heated to more than 30 ℃ dissolves, the solution after will dissolving is poured in the 150mm pottery ware, place again baking oven slowly heating evaporation keep half an hour to doing for 300 ℃ in temperature.Get anhydrous chlorides of rase calcium product 57g in the pottery ware, product color is pure white.Get Calcium Chloride Powder Anhydrous sample 1g, with adopting the HJ/T132-2003 standard behind the distilled water diluting, the potassiumiodide basic potassium permanganate method is measured CODcr, measures to obtain that CODcr content is 0.15% in this anhydrous chlorides of rase calcium product.
Comparative example 2 and the result of embodiment 6 show, adopt method of the present invention to handle described processing wastewater, the content comparison of the organic pollutant of resultant anhydrous chlorides of rase calcium product is more much lower than the content of the organic pollutant of embodiment 2 resultant anhydrous chlorides of rase calcium products.Therefore, method of the present invention is a kind of epoxy chloropropane productive rate height, the environment amenable method of by product.
Claims (9)
1. the production method of an epoxy chloropropane is characterized in that the step of this method is as follows:
With the dichloropropanol isomer mixed solution of 900-1000 weight part, the water of 950-1050 weight part, the HCl of 70-100 weight part and the Ca (OH) of 2600-2800 weight part
2Content is that the lime slurry of 12-18 weight % mixes, and is added to reactive distillation column top behind the mixing; Described Ca (OH)
2The particulate specific surface area is 200-2100m
2/ kg, median size 1.8-20.0 μ m;
The water vapor that feeds the 1100-1300 weight part at the bottom of described reactive distillation column makes dehydrochlorination saponification cyclization reaction product carry out stripping, simultaneously described reaction distillation capital temperature is controlled at 86-90 ℃;
Then, collect described reaction distillation column top fractions, and in condenser, carry out condensation, obtain phlegma; Cut is for containing CaCl at the bottom of the described reactive distillation column
2, glycerine and organochlorine processing wastewater, handle;
Described phlegma is separated, and obtains containing the organic phase and the aqueous water of epoxy chloropropane, and described water turns back in the described reactive distillation column;
Then, described organic phase sent among the knockout tower I under absolute pressure 0.12-0.14MPa condition, separate, isolate light by-product and be rich in the product of epoxy chloropropane; Described light by-product is discharged from knockout tower I cat head, discharges at the bottom of this tower as tower bottom distillate and be rich in epichlorohydrin product, and described tower bottom distillate is again by being pumped into knockout tower II;
Described tower bottom distillate separates under absolute pressure 36-40KPa condition in described knockout tower II, isolates residual light by-product, pure epoxy chloropropane product and heavy by product; Described residual light by-product is discharged from knockout tower II cat head, and described pure epoxy chloropropane is discharged from knockout tower II tower side, is target product of the present invention, and described heavy byproduct waste liquid is discharged at the bottom of the knockout tower II tower and handled.
2. method according to claim 1, it is characterized in that described dichloropropanol isomer mixed solution is the product that the glycerine method is produced dichlorohydrine, this mixture contains in 1 of its mixture total weight amount 95-98 weight %, the 2.3-two trimethylewne chlorohydrin 3-isomer of 3-two chloro-2-propyl alcohol isomer and 2-5 weight %.
3. method according to claim 1 is characterized in that described Ca (OH)
2The particulate specific surface area is 726-765m
2/ kg.
4. method according to claim 1 is characterized in that described Ca (OH)
2The median size of particulate is 5.3-4.6 μ m.
5. method according to claim 1 is characterized in that described processing wastewater processing is as follows:
Described processing wastewater carries out evaporation concentration by quintuple effect evaporator earlier, is concentrated into calcium chloride content and reaches in concentrating spent liquor gross weight 50 weight %CaCl
2
The concentrating spent liquor that obtains carries out crystallisation by cooling, separates out the calcium chloride hexahydrate crystal, carries out filtering separation then;
Separate the calcium chloride hexahydrate crystal that obtains and heat, obtain calcium chloride water, carry out spraying drying again, obtain Calcium Chloride Powder Anhydrous;
Simultaneously, separate the crystalline mother solution that contains glycerine and organic chloride that obtains and carry out burning disposal.
6. method according to claim 5, it is characterized in that it is 0.7-0.9MPa that described quintuple effect evaporator uses the absolute pressure of heating steam, the secondary steam absolute pressure of quintuple effect evaporator is 0.018-0.022MPa, the total temperature difference of described quintuple effect evaporator is 108-109 ℃, 52.5-53.5 ℃ of total temperature difference loss, effective temperature difference 54.5-56.5 ℃.
7. method according to claim 5 is characterized in that described concentrating spent liquor carries out crystallisation by cooling under temperature 15-21 ℃.
8. method according to claim 5 is characterized in that described calcium chloride hexahydrate crystal heated 20-30 minute down at temperature 30-35 ℃, obtained calcium chloride water.
9. method according to claim 5 is characterized in that described calcium chloride solution carries out spraying drying in 350 ℃ of temperature and gauge pressure 50-200pa direct draught.
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Effective date of registration: 20101115 Address after: 315812 Zhejiang city of Ningbo province Donggang Daxie Development Zone No. 1 North Road, No. 206, room 208, office building Applicant after: Ningbo Huanyang Chemical Co., Ltd. Address before: 315812 Zhejiang city of Ningbo province Donggang Daxie Development Zone No. 1 North Road Applicant before: Ningbo Donggang Electrochemical Co., Ltd. |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP03 | Change of name, title or address |
Address after: 318512 Zhejiang city of Ningbo province Beilun Daxie Development Zone Donggang Road No. 7 Patentee after: Ningbo new materials Limited by Share Ltd Address before: 315812 Zhejiang city of Ningbo province Donggang Daxie Development Zone No. 1 North Road, No. 1, office building 206, room 208 Patentee before: Ningbo Huanyang Chemical Co., Ltd. |